CN111943426A - Treatment method of high-salt-content pharmaceutical wastewater - Google Patents
Treatment method of high-salt-content pharmaceutical wastewater Download PDFInfo
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- CN111943426A CN111943426A CN202010659940.7A CN202010659940A CN111943426A CN 111943426 A CN111943426 A CN 111943426A CN 202010659940 A CN202010659940 A CN 202010659940A CN 111943426 A CN111943426 A CN 111943426A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
Abstract
The invention discloses a method for treating pharmaceutical wastewater with high salt content, and belongs to the technical field of wastewater treatment. The method of the invention sequentially leads the high-salt pharmaceutical wastewater into the coagulating sedimentation tank, the anaerobic bioreactor filled with scrap iron and granular activated carbon and the dynamic membrane treatment system adopting photosynthetic bacteria to culture bacteria for coagulating sedimentation pretreatment, anaerobic treatment and aerobic advanced treatment, thereby not only enhancing the biochemical performance of the wastewater, improving the treatment efficiency of the wastewater and realizing the standard discharge of the wastewater, but also having simple process and low energy consumption.
Description
Technical Field
The invention relates to a method for treating pharmaceutical wastewater with high salt content, and belongs to the technical field of wastewater treatment.
Background
Water is one of the most valuable resources for human beings, and the development and progress of human beings can not leave the water resource. In recent times, the problem of water resource pollution caused by the acceleration of the industrialization process becomes more and more serious, the development of economy in China is restricted, the health of people is threatened, and the sustainable development of the society is not facilitated. According to statistics, the existing pharmaceutical enterprises in China are nearly 5000 families, the discharge amount of wastewater reaches 0.25Gt, and the treatment rate is less than 30%. The pharmaceutical products are various in types, the components of the generated pharmaceutical wastewater are complex, and the concentration and the salt content of organic matters are extremely high. On one hand, with the shortage of water resources and the rapid deterioration of the environment, the effective treatment and the maximum recycling of the high-salinity pharmaceutical wastewater are more and more paid attention by people; on the other hand, the high-salt pharmaceutical wastewater poses a great threat to the living environment of human beings, and how to effectively solve the problem of purification treatment of the high-salt pharmaceutical wastewater becomes a central importance in national environmental management.
At present, the method for treating pharmaceutical wastewater at home and abroad mainly comprises the following steps: chemical methods (such as iron-carbon micro-electrolysis, Fenton oxidation and the like), physical and chemical methods (such as coagulation, adsorption, membrane separation and the like), biological methods (such as aerobic biological treatment, anaerobic biological treatment and the like). The chemical method or the physical chemical method is independently adopted to cause the problems of large dosage, easy generation of secondary pollution and the like; the high-salinity pharmaceutical wastewater is difficult to directly adopt biological treatment, and the effluent quality is difficult to reach the standard. At present, the high-salt pharmaceutical wastewater is generally treated by combining a plurality of technologies, but the conventional treatment method has the problems of complex and unstable process flow, high treatment cost, low efficiency and the like. Therefore, a processing system with simple flow, high processing efficiency and low energy consumption is required.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a method for treating pharmaceutical wastewater with high salt content, which comprises the steps of sequentially introducing the pharmaceutical wastewater with high salt content into a coagulating sedimentation tank, an anaerobic bioreactor filled with scrap iron and granular activated carbon and a dynamic membrane treatment system using photosynthetic bacteria as strains for treatment, so that the biochemical performance of the wastewater can be enhanced, the treatment efficiency of the wastewater is improved, the standard discharge of the wastewater is realized, the process is simple, and the energy consumption is low.
In order to achieve the technical purpose, the technical scheme of the invention is as follows:
a treatment method of high-salt pharmaceutical wastewater comprises the following steps:
(1) introducing the high-salt pharmaceutical wastewater into a coagulating sedimentation tank, adding a coagulant into the coagulating sedimentation tank, and carrying out coagulating sedimentation pretreatment;
(2) introducing the effluent of the coagulation sedimentation tank into a UASB anaerobic bioreactor for anaerobic treatment, wherein scrap iron and granular activated carbon are uniformly distributed in anaerobic sludge in the UASB anaerobic bioreactor;
(3) and (3) introducing the effluent of the anaerobic bioreactor into a dynamic membrane system for aerobic advanced treatment, wherein photosynthetic bacteria are adopted as strains in the dynamic membrane system, and the treated effluent is directly discharged.
Preferably, the total salt content in the high-salt pharmaceutical wastewater in the step (1) is 1-5%.
Preferably, the coagulant in step (1) is one or a mixture of more of polyaluminium chloride, polyferric chloride, polyaluminium sulfate, polyferric sulfate and polyacrylamide.
Preferably, the hydraulic retention time of the high-salt pharmaceutical wastewater in the coagulating sedimentation tank in the step (1) is 1-2 h, and the pH value of the effluent of the coagulating sedimentation tank is controlled to be 7.0-8.0.
Preferably, the inoculation ratio of the anaerobic sludge in the step (2) is 3:1, 5-20 g of scrap iron and 2-10 g of granular activated carbon are filled in every 1L of anaerobic sludge.
Preferably, in the step (2), the hydraulic retention time of the effluent of the coagulation sedimentation tank in the anaerobic bioreactor is 24-48 h, and the temperature in the anaerobic bioreactor is controlled at 35 ℃.
Preferably, in the step (3), the effluent of the anaerobic bioreactor stays in the dynamic membrane system for 5-10 hours in a hydraulic manner, and the concentration of dissolved oxygen in the dynamic membrane system is controlled to be 1-3 mg/L.
Preferably, the photosynthetic bacteria described in step (3) are selected from seawater.
Preferably, the dynamic membrane module in the dynamic membrane system described in step (3) adopts a stainless steel net or a non-woven fabric as a dynamic supporting base net, and the dynamic membrane is installed in a submerged manner.
From the above description, it can be seen that the present invention has the following advantages:
(1) the method of the invention sequentially introduces the high-salt pharmaceutical wastewater into the coagulating sedimentation tank, the anaerobic bioreactor filled with scrap iron and granular activated carbon and the dynamic membrane treatment system adopting the photosynthetic bacteria to culture the wastewater for treatment, thereby not only enhancing the biochemical performance of the wastewater, improving the treatment efficiency of the wastewater and realizing the standard discharge of the wastewater, but also having simple process and low energy consumption.
(2) The invention homogenizes scrap iron and granular activated carbon in anaerobic sludge in the anaerobic bioreactor, and is beneficial to the enrichment of characteristic microorganisms in the anaerobic bioreactor, thereby promoting the electron transfer efficiency in the anaerobic reaction process, enhancing the biochemical performance of wastewater and improving the wastewater treatment efficiency.
(3) The invention adopts the high-salt-tolerance photosynthetic bacteria screened by seawater as the strains in the dynamic membrane treatment system, can effectively improve the treatment efficiency of the wastewater, is beneficial to the advanced treatment of the wastewater, adopts the dynamic membrane to carry out the solid-liquid separation of the photosynthetic bacteria, has long operation period and controllable membrane pollution.
Detailed Description
The features of the invention will be further elucidated by the following examples, without limiting the claims of the invention in any way.
Example 1
A treatment method of high-salt pharmaceutical wastewater comprises the following steps:
(1) introducing high-salt pharmaceutical wastewater with the total salt content of 1.5% into a coagulative precipitation tank, adding polyaluminium chloride into the coagulative precipitation tank, wherein the adding amount of the polyaluminium chloride is 60mg/L of the wastewater, and performing coagulative precipitation pretreatment, wherein the hydraulic retention time of the wastewater in the coagulative precipitation tank is 2 hours, and the pH of the effluent of the coagulative precipitation tank is controlled at 7.0;
(2) introducing the effluent of the coagulation sedimentation tank into a UASB anaerobic bioreactor to perform anaerobic treatment at 35 ℃, wherein the hydraulic retention time of the effluent of the coagulation sedimentation tank in the anaerobic bioreactor is 48h, scrap iron and granular activated carbon are uniformly distributed in the anaerobic sludge in the UASB anaerobic bioreactor, the inoculation ratio of the anaerobic sludge (the volume ratio of the anaerobic sludge to the wastewater) is 3.0:1, the concentration of the scrap iron is 12g/L of the anaerobic sludge, the concentration of the granular activated carbon is 3g/L of the anaerobic sludge, and the mass ratio of the scrap iron to the granular activated carbon is 4: 1;
(3) introducing the effluent of the anaerobic bioreactor into a dynamic membrane system for aerobic advanced treatment, and directly discharging the treated effluent; the method is characterized in that the hydraulic retention time of effluent of an anaerobic bioreactor in a dynamic membrane system is 10 hours, the concentration of dissolved oxygen in the dynamic membrane system is controlled to be 2mg/L, a dynamic membrane component in the dynamic membrane system adopts a stainless steel net as a dynamic supporting base net, the dynamic membrane is installed in a submerged mode, photosynthetic bacteria are adopted as strains in the dynamic membrane system, the photosynthetic bacteria are screened from seawater, and the screening method refers to a method in a document [ Hushu Wen, culture optimization of the photosynthetic bacteria and biological enhanced treatment garbage percolate effect research [ D ]. Chongqing university, 2018 ]2.1, and the difference is only that garbage percolate is replaced by seawater.
The wastewater in this example was distributed by laboratory water, and the water quality of the inlet and outlet water in each step of this example is shown in table 1:
TABLE 1
Example 2
The same method as that used in example 1 was used, except that pharmaceutical wastewater from Shanghai was used as the wastewater in this example, and the water quality of the inlet and outlet water in the steps of this example is shown in Table 2:
TABLE 2
Comparative example 1
The same procedure as in example 2 was followed except that the anaerobic sludge was inoculated at a ratio of 2.5:1, the iron filings concentration was 12g/L anaerobic sludge, the granular activated carbon concentration was 4g/L anaerobic sludge, and the mass ratio of the iron filings to the granular activated carbon was 3: 1. The water quality of the inlet and outlet water in each step of this example is shown in table 3:
comparative example 2
The same procedure as in example 2 was followed, except that the inoculation ratio of anaerobic sludge was 3.5:1, the iron filings concentration was 9g/L anaerobic sludge, the granular activated carbon concentration was 2g/L anaerobic sludge, and the mass ratio of iron filings to granular activated carbon was 4.5: 1. The water quality of the inlet and outlet water in each step of this example is shown in table 4:
it should be understood that the detailed description of the invention is merely illustrative of the invention and is not intended to limit the invention to the specific embodiments described. It will be appreciated by those skilled in the art that the present invention may be modified or substituted equally as well to achieve the same technical result; as long as the use requirements are met, the method is within the protection scope of the invention.
Claims (9)
1. The method for treating the high-salt pharmaceutical wastewater is characterized by comprising the following steps of:
(1) introducing the high-salt pharmaceutical wastewater into a coagulating sedimentation tank, adding a coagulant into the coagulating sedimentation tank, and carrying out coagulating sedimentation pretreatment;
(2) introducing the effluent of the coagulation sedimentation tank into a UASB anaerobic bioreactor for anaerobic treatment, wherein scrap iron and granular activated carbon are uniformly distributed in anaerobic sludge in the UASB anaerobic bioreactor;
(3) and (3) introducing the effluent of the anaerobic bioreactor into a dynamic membrane system for aerobic advanced treatment, wherein photosynthetic bacteria are adopted as strains in the dynamic membrane system, and the treated effluent is directly discharged.
2. The treatment method of claim 1, wherein the total salt content in the high-salt pharmaceutical wastewater in the step (1) is 1-5%.
3. The treatment method according to claim 1, wherein the coagulant in step (1) is one or more of polyaluminium chloride, polyferric chloride, polyaluminium sulfate, polyferric sulfate and polyacrylamide.
4. The treatment method according to claim 1, wherein the hydraulic retention time of the high-salt pharmaceutical wastewater in the coagulative precipitation tank in the step (1) is 1-2 h, and the pH of the effluent of the coagulative precipitation tank is controlled to be 7.0-8.0.
5. The treatment method according to claim 1, wherein the inoculation ratio of the anaerobic sludge in the step (2) is 3:1, 5-20 g of scrap iron and 2-10 g of granular activated carbon are filled in each 1L of anaerobic sludge.
6. The treatment method according to claim 1, wherein in the step (2), the hydraulic retention time of the effluent of the coagulation sedimentation tank in the anaerobic bioreactor is 24-48 h, and the temperature in the anaerobic bioreactor is controlled at 35 ℃.
7. The treatment method according to claim 1, wherein in the step (3), the effluent of the anaerobic bioreactor is hydraulically retained in the dynamic membrane system for 5-10 h, and the concentration of dissolved oxygen in the dynamic membrane system is controlled to be 1-3 mg/L.
8. The process of claim 1, wherein the photosynthetic bacteria in step (3) are selected from seawater.
9. The process of claim 1, wherein the dynamic membrane module in the dynamic membrane system in step (3) uses stainless steel mesh or non-woven fabric as a dynamic supporting base mesh, and the dynamic membrane is installed by flooding.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050109694A1 (en) * | 2003-11-21 | 2005-05-26 | Industrial Technology Research Institute | Method and system for treating wastewater containing organic compounds |
| CN101624250A (en) * | 2009-06-27 | 2010-01-13 | 大连理工大学 | Anaerobic zero-valent iron sewage treatment method |
| CN102363546A (en) * | 2011-06-20 | 2012-02-29 | 上海明诺环境科技有限公司 | High salinity pharmaceutical wastewater processing system |
| CN102372401A (en) * | 2011-09-28 | 2012-03-14 | 同济大学 | Iron-carbon micro-electrolysis-dynamic membrane wastewater deep treatment process |
| CN103739142A (en) * | 2013-11-15 | 2014-04-23 | 安徽省绿巨人环境技术有限公司 | Chinese patent medicine production wastewater treatment technology |
| CN110550736A (en) * | 2019-10-17 | 2019-12-10 | 中国科学院城市环境研究所 | Method for pretreating high-concentration fluoroquinolone antibiotic wastewater by using iron-carbon microelectrolysis coupling anaerobic acid production fermentation process |
| CN110803764A (en) * | 2019-12-02 | 2020-02-18 | 江苏蓝必盛化工环保股份有限公司 | Device for treating chemical wastewater by using zero-valent iron reinforced ABR (anaerobic baffled reactor) |
-
2020
- 2020-07-10 CN CN202010659940.7A patent/CN111943426B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050109694A1 (en) * | 2003-11-21 | 2005-05-26 | Industrial Technology Research Institute | Method and system for treating wastewater containing organic compounds |
| CN101624250A (en) * | 2009-06-27 | 2010-01-13 | 大连理工大学 | Anaerobic zero-valent iron sewage treatment method |
| CN102363546A (en) * | 2011-06-20 | 2012-02-29 | 上海明诺环境科技有限公司 | High salinity pharmaceutical wastewater processing system |
| CN102372401A (en) * | 2011-09-28 | 2012-03-14 | 同济大学 | Iron-carbon micro-electrolysis-dynamic membrane wastewater deep treatment process |
| CN103739142A (en) * | 2013-11-15 | 2014-04-23 | 安徽省绿巨人环境技术有限公司 | Chinese patent medicine production wastewater treatment technology |
| CN110550736A (en) * | 2019-10-17 | 2019-12-10 | 中国科学院城市环境研究所 | Method for pretreating high-concentration fluoroquinolone antibiotic wastewater by using iron-carbon microelectrolysis coupling anaerobic acid production fermentation process |
| CN110803764A (en) * | 2019-12-02 | 2020-02-18 | 江苏蓝必盛化工环保股份有限公司 | Device for treating chemical wastewater by using zero-valent iron reinforced ABR (anaerobic baffled reactor) |
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